KR20010056962A - Method of treating dye containing waste water - Google Patents

Abstract

PURPOSE: A method of dyeing wastewater is provided, which can reduce color intensity effectively and decompose nonbiodegradable polymer organics contained in dyeing wastewater, by an upflow anaerobic sludge blanket process (UASB) and so can discharge treated water of good quality. CONSTITUTION: The method comprises as follows: (i) adjust the pH of dyeing wastewater; (ii) hydrolyze and ferment organic acid of the pH adjusted dyeing wastewater through an upflow anaerobic sludge blanket process (UASB) (2); (iii) contact the dyeing wastewater passed the UASB to air at an air contact tank (3); (iv) hydrolyze and ferment organic acid of the air contacted dyeing wastewater through an upflow packed bed bioreactor (UFPB) (4); and (v) aerobic treat the wastewater passed the UFPB (4) at an aeration tank (5); (vi) coagulate the aerobic treated wastewater at a coagulation tank (7).

Description

Method of treating dye containing waste water

[TECHNICAL FIELD OF THE INVENTION]

The present invention relates to a dyeing wastewater treatment method, and more particularly, to an economical and highly efficient dyeing wastewater treatment method for treating a dyeing wastewater containing a large amount of hardly decomposable organic compounds.

[Private Technology]

Characteristics of Dye Wastewater

In general, dyeing wastewater refers to wastewater generated through starch removal, refining, bleaching, polishing, dyeing, and finishing, which are components of the dyeing and cleaning industry. Dyeing wastewater has high fluctuations in the amount of water generated and water quality, and high concentrations of hardly decomposable organic compounds such as dyes, PVA, synthetic detergents, and scavengers. It has characteristics of high temperature (40 ℃) and strong alkali (pH 11 ~ 12.5). I have it.

Table 1 summarizes the characteristics of the dye contained in the dye wastewater.

division Dye Classification Main target fiber, material Chemical structure, staining features Water-insoluble Disperse Dyes Polyester Absorption in conjugated double bond UV region in dye molecules by insoluble and dispersing system Disperse Fluorescent Dyes Polyester Water Soluble Dye Cationic dye Acrylic, CDP Quaternary ammonium salt or carbonium group Acid dyes Nylon, silk, wool Sulfonic acid Acid dyes containing metal Nylon, wool Chromium, cobalt complex structure Direct dyes Cotton, rayon, paper Polyazo, Sulfonate Reactive dyes Cotton rayon Reactor (reaction with -OH), sulfonic acid group Sulfide dyes Cotton rayon Reduction with Na ₂ S. Dissolution Dyeing Water soluble fluorescent dyes Cotton, paper, detergent Stilben structure, conjugated double bond Reducing dyes - Vat dyes

In addition, organic compounds must include chromophores and chromophores in order to be used as dyes. Chemical structures of representative dyes are shown in Table 2 below.

In addition, the types of chromophores and chromophores included in the dye are as follows.

[Chromophore]

Azo nitro carbonyl

[Color palette]

Amino hydroxy

-NH ₂ -OH

Conventional dye wastewater treatment method and its problems

Conventional dye wastewater treatment consists of aeration (activated sludge) for organic matter removal, chemical oxidation for removal of hardly decomposable substances and discoloration. An example of a typical dyeing wastewater treatment process in Korea is shown in FIG. 1.

Problems of the conventional dyeing wastewater treatment process as shown in Figure 1 can be summarized as an excessive amount of chemicals, a large amount of sludge, nevertheless poor treatment water quality.

In the case of Ansan B dyeing complex in FIG. 1, since the process of neutralizing the strong alkaline wastewater of pH 12 or more to pH 7 by adding H ₂ SO ₄ to form a favorable condition for the aerobic biological treatment of the latter stage is used for pH adjustment The drug costs become excessive. Meanwhile, the Fenton oxidation method applied after the aerobic treatment of the pure oxygen aeration method is a method of removing hardly decomposable organic matter and color using hydrogen peroxide (H ₂ O ₂ ) as an oxidizing agent and iron salt (FeCl ₂ ) as a catalyst under acidic conditions. Fenton oxidation process is an organic substance, and overall maintenance costs are excessive issue price is expensive and the effective, but the hydrogen peroxide (H ₂ O ₂₎ as well as being an oxidizing agent to the sludge production occurs in large quantities of sludge treatment cost increase than the normal flocculation on Color Removal .

In addition, in the case of Daegu K in Figure 1, MgCl ₂ coagulation sedimentation method that maintains the proper treatment efficiency in the high pH range was applied, in which case HCl is generated through the reaction with water, the pH is lowered, so the pH is added by NaOH It is operating in an ascending manner. This method has a problem in that the amount of chemicals is excessively increased and sludge generation is increased as well as the chemical cost for pH adjustment is increased by directly flocculating sedimentation of the raw wastewater with high pollution concentration.

In addition, the chlorine-based oxidation method applied as a post-treatment mainly uses the hydrochloric acid, bleaching powder, etc., the color removal of the waste water by the bleaching action is mainly ineffective for the removal of hardly decomposable organic matter. Decolorization by the chlorine-based oxidation method has a low color removal rate, there is a problem in that the use of the color due to the side effect of the decolored color is restored or rather the coloration is increased. In particular, it is very likely that the decolorant reacts with the organic material in the dyeing wastewater to produce organic chloride, which is a toxic environmental hormone substance, through the path as in Scheme 1 below.

Scheme 1

On the other hand, the pure oxygen aeration and activated sludge method used in the biological treatment method in the two processes of Figure 1 is an effective organic material removal method for general sewage treatment, but very inadequate for the treatment of hardly degradable wastewater containing a large amount of organic polymer compounds, such as dyeing wastewater That's the way. For example, in the case of dyed wastewater, the CODcr representing the total organic concentration is about 2,000 mg / l, whereas the BOD representing the organic concentration that is easily biodegradable is only 100 mg / l. In other words, most of the organic matter contained in the dye wastewater is not able to achieve an appropriate level of treatment effect by the general biological treatment.

In addition, since the water quality and quantity fluctuate depending on the process configuration and operating time of each dyeing plant, there is no guarantee that a successful wastewater treatment method in one plant will succeed in another plant. Therefore, there is an urgent need for the invention of a universal wastewater treatment method that is suitable for the overall characteristics of dyeing wastewater and can flexibly cope with variations in water quality and quantity.

In order to solve the above problems, the present invention converts the non-degradable organic material of the dyeing wastewater into an easily decomposable substance in the anaerobic biological treatment, removes the chromaticity-inducing substance, and then, the dyeing wastewater through the aerobic treatment process and the coagulation sedimentation process. The aim is to provide a method for treating dyed wastewater in an efficient and economical way, while flexibly coping with fluctuations in water quality and quantity.

1 is a conventional dyeing wastewater treatment method,

2 is a process chart of the dyeing wastewater treatment method using a two-stage upflow anaerobic sludge blanket process as a main process;

3 is a process diagram of the dyeing wastewater treatment method using the upflow anaerobic sludge blanket process and the upflow packed bed bioreactor as main processes,

4 is a result of qualitative change in chromaticity and pH of the dyeing wastewater according to Example 1,

Figure 5 shows a schematic diagram of the process applied in Example 2,

Figure 6 is the result of analyzing the dye wastewater absorbance of each step in Example 2.

In order to achieve the above object, the present invention is (a) adjusting the pH of the introduced dye wastewater, (b) hydrolysis and organic acid fermentation through the first upflow anaerobic sludge blanket process for adjusting the pH (C) contacting the dyed wastewater that has passed through the first upflow anaerobic sludge blanket process with air, and (d) hydrolyzing the dyed wastewater in contact with the air through a second upflow anaerobic sludge blanket process. And fermenting an organic acid, (e) aerobic treatment of the dyed wastewater that has passed the second upflow anaerobic sludge blanket process, and (f) flocculating the aerobic dyed wastewater. Dye wastewater treatment method is provided.

In another aspect, the present invention (a) adjusting the pH of the dyeing wastewater containing a large amount of reducing dye introduced, (b) hydrolysis and organic acid fermentation through the first upflow anaerobic sludge blanket process for adjusting the pH (C) hydrolysing and organic acid fermenting the dyeing wastewater passed through the first upflow anaerobic sludge blanket process through a second upflow anaerobic sludge blanket process, and (d) the second upflow anaerobic sludge blanket process It provides a dyeing wastewater treatment method comprising the step of aerobic treatment of the dyeing wastewater that has passed the process and (e) agglomerated sedimentation of the aerobic treated dyeing wastewater.

In another aspect, the present invention (a) adjusting the pH of the dyeing wastewater introduced, (b) hydrolyzing and organic acid fermentation through the first upflow anaerobic sludge blanket process for adjusting the pH, (c) Contacting the dyed wastewater that has passed through the first upflow anaerobic sludge blanket process with air, (d) hydrolyzing and organic acid fermenting the dyed wastewater in contact with the air in an upflow packed bed bioreactor and (e) It provides a dyeing wastewater treatment method comprising the step of aerobic treatment of the dyeing wastewater passed through the upflow packed bed bioreactor.

Hereinafter, the present invention will be described in detail.

The dyeing wastewater treatment method of the present invention is hydrolyzed and organic acid fermentation process using the primary and secondary upflow anaerobic sludge blanket process (hereinafter referred to as "UASB") by adjusting the pH of the introduced dye wastewater. Through the conversion of the hardly decomposable substance into an easily decomposable substance, the color-inducing substance is removed. Subsequently, organic substances converted to easy decomposition are removed in a continuous aerobic biological process, and residual organic substances and chromaticity-inducing substances are finally removed through a coagulation sedimentation process at a later stage. Figure 2 shows a schematic process diagram of the dye wastewater treatment method.

In addition, in the dyeing wastewater treatment method of the two-stage UASB process, the step of contacting the dyeing wastewater passing through the primary UASB with air does not include an air contacting step when the dyeing wastewater contains a large amount of reducing dye. Reducing dyes do not have a sulfone group, so the degree of pH decrease due to hydrolysis is insignificant. Therefore, the negative effect of recoloring the wastewater is greater than the positive effect of raising the pH through the air contact step.

In addition, another dyeing wastewater treatment method of the present invention is treated with UASB by adjusting the pH of the inflowing dyeing wastewater, followed by an Upflow Packed-bed Bioreactor (hereinafter referred to as "UFPB") filled with waste granular activated carbon. By strengthening the hydrolysis and organic acid fermentation process, the hardly decomposable substance is converted into an easily decomposable substance, and the color removing agent is removed. Subsequent aerobic biological processes remove the organic material that has been converted to easy decomposition. In addition, in the dyeing treatment method, a flocculation sedimentation process may be applied to secure a safe treatment water quality. Figure 3 shows a schematic process diagram of the dye wastewater treatment method.

Anaerobic microorganisms are characterized by high degradability to hardly decomposable substances and strong resistance to toxic substances. Anaerobic biological treatment can simply be defined as the process in which organic matter is decomposed into CO ₂ and CH ₄ in the absence of oxygen, but in reality it is a complex reaction in which the reaction pathway and related microorganisms are not precisely identified. In general, anaerobic decomposition consists of hydrolysis, acid formation, and methane formation process, which requires a very long residence time in order to proceed to the methane formation process.

In the present invention, the main process is to remove the color causing agent and convert the hardly decomposable substance into an easily decomposable substance by proceeding only to the hydrolysis and acid formation step in the anaerobic treatment process, and utilize the following treatment mechanism.

Hydrolysis of sulfone groups

Water-soluble dyes containing a hydrophilic functional sulfone group (-SO ₃ Na) are converted to water insoluble as the sulfone group is removed by anaerobic hydrolysis. As the dye molecules of the polymer are converted into water-insoluble, they precipitate as precipitates, and the low-molecular dye molecules become colloidal materials that can be easily removed by chemical flocculation. On the other hand, pH is lowered by the produced NaSO ₄ . The reaction process is the same as in Scheme 2.

Scheme 2

Acid Fermentation of Organics

Other undegradable organics in the dye wastewater are fermented into organic acids by the same route as in Scheme 3 below to produce by-products of hydrogen (H ₂ ) and CO ₂ .

Scheme 3

C ₆ H ₁₂ O ₆ + 2H ₂ O → 2CH ₃ COOH + 4H ₂ + 2CO ₂

Reduction bleaching of azo dyes

Azo groups, which are the main coloring functional group of the dye, are decolorized by decomposition by a reduction reaction combined with hydrogen, and the reaction process is shown in Scheme 4 below.

Scheme 4

Reduction of Sulfuric Acid

The SO ₄ ^-2 produced by the hydrolysis is converted to S ⁻ by a path of the following Reaction Scheme 5 while reducing the reaction by the organic acid and the sulfur reducing bacterium.

Scheme 5

^{_{CH 3 COOH + SO 4 -2 →}} CO 2 + HS - + HCO 3 - + H 2 O

H ₂ Oxidation of S

S ⁻ produced by the sulfur reduction reaction is oxidized to S solids by the dissolved oxygen in water through the route of Scheme 6 below. It is preferable to include contacting the dyeing wastewater with air between the primary UASB and the secondary UASB for the progress of the reaction.

Scheme 6

2H ₂ S + O ₂ → 2H ₂ O + 2S ↓

Looking at the steps included in the present invention in detail.

pH adjustment step (1 in FIG. 2, 1 in FIG. 3)

In general, a suitable pH range for anaerobic treatment is known to be neutral, but the optimal pH range for hydrolysis of the dyeing wastewater containing sulfone groups is 9-10. The main reason why the anaerobic process was excluded in the treatment of dye wastewater in the past is that the pH of the wastewater is more than 12 and lowers the wastewater to pH 7 which is known to be suitable for the anaerobic process. Because it was low. Therefore, the present invention accurately grasps the characteristics of the dyeing wastewater, and lowers the wastewater of pH 12 or more to pH 9 to 10 to reduce the amount of chemical consumption while providing optimum conditions for hydrolysis of the sulfone group-containing organic matter.

Hydrolysis and Organic Acid Fermentation in Primary UASB (2 in FIG. 2, 2 in FIG. 3)

The pH of the wastewater adjusted to 9-10 is hydrolyzed under anaerobic conditions for up to 4 hours of residence time. CODcr removal rate in this process is 25 to 30%, chromaticity removal rate is 70 to 80%. The reason why the CODcr removal rate is low in this step is to convert the hardly decomposable organic material into easy decomposition state through hydrolysis and to remove it in large quantities in the subsequent aerobic treatment, and aims to completely remove the CODcr after a long residence time in UASB. Because it does not. In this step, the color removal rate reaches 70 to 80% because the dye molecules are converted into dye intermediates by hydrolysis. In addition, as the sulfone group is removed in this step, the dye molecules converted into water-insoluble precipitate as precipitates. Also, in this step, the black dye wastewater is converted to yellow or brown dye intermediate through the first UASB, thus becoming orange.

Air contact step (3 in FIG. 2, 3 in FIG. 3)

When anaerobic hydrolysis of the dyeing wastewater proceeds in the first UASB, NaHSO ₄ is generated to lower the pH. In addition, SO ₄ ^-2 generated in hydrolysis forms a large amount of H ₂ S by organic acids and sulfur reduction bacteria. Since H ₂ S lowers pH and causes toxicity to microorganisms, the primary UASB effluent is introduced into the air contact tank to oxidize H ₂ S and then supplied to the secondary UASB. The primary UASB effluent, reduced to pH 7, rises to pH 8.5 through an air contact bath.

On the other hand, when a large amount of reducing dyes (Vat dyes) are contained in the dyeing waste water, it is advantageous not to install an air contact tank. The reducing dye reacts with H ₂ in the anaerobic state to be reduced and then hydrolyzed, which takes a long time for hydrolysis. Reducible dyes are reduced in color by reduction, but the color is restored when they are oxidized in contact with air before complete hydrolysis. In addition, the reducing dye does not have a sulfonic group, so the degree of pH decrease due to hydrolysis is insignificant. Therefore, it may be said that the negative effect of recoloring the wastewater is greater than the positive effect of raising the pH by installing an air contact tank.

The change in molecular structure and color according to redox reaction of Indigosol O, a typical reducing dye, is shown in Scheme 7 below.

Scheme 7

Hydrolysis and Organic Acid Fermentation in Secondary UASB (4 in FIG. 2)

This step is to proceed anaerobic hydrolysis and organic acid fermentation for the air contact tank effluent, and the main purpose is to remove the amino group, which is similar in function to the primary UASB, but is crude. The residence time of this process is preferably up to 10 hours, and removes about 25 to 30% of the CODcr of the incoming air contact tank effluent. The CODcr removal rate is 45 to 50% and the chromaticity removal rate is about 80% compared to the raw waste water of the first UASB and the second UASB.

Hydrolysis and Organic Acid Fermentation in UFPB (4 in FIG. 3)

The UFPB applied in the present invention is preferably UFPB filled with activated carbon, and the activated carbon may be granular activated carbon discarded after use in an air pollution prevention facility. When activated carbon is charged, microorganisms necessary for anaerobic decomposition accumulate in activated carbon to form biofilms and adsorb organic substances. As a result, the organic matter is concentrated in the reactor, which increases the actual residence time of the contaminants. The contaminants are continuously subjected to hydrolysis and organic acid fermentation by microorganisms accumulated in high concentration on activated carbon. In particular, the use of UFPB is effective in the case of waste water containing a large amount of reducing dyes, which requires a long time for anaerobic hydrolysis.

Aerobic treatment steps (5 and 6 of FIG. 2, 5 and 6 of FIG. 3)

In the first and second UASB process or UASB and UFPB process, a large amount of organic matter changed to an easily decomposable substance through anaerobic hydrolysis and organic acid fermentation is removed in aerobic state. At this time, the aerobic treatment process can be used such as general activated sludge or SBR (continuous batch reactor). The hydraulic residence time of the aerobic treatment process is up to 12 hours and removes about 80% of the CODcr contained in the secondary UASB effluent, and the chromaticity is not removed through this process. The CODcr removal rate is 85 to 90% of the raw waste water of the treated water after the first and second UASB and aerobic treatment processes.

In the present invention, the dye wastewater treatment process is composed of aerobic treatment after anaerobic treatment to change the properties of the surfactant in the anaerobic treatment of the surfactant contained in the dyeing wastewater does not generate bubbles during aerobic treatment. Existing dyeing wastewater treatment process that performs aerobic treatment without anaerobic treatment causes operational problems due to excessive foaming.

Coagulation sedimentation process (7 and 8 of Figure 2, 7 and 8 of Figure 3)

In case of directly flocculating sedimentation wastewater, suspended solids and colloidal substances can be removed, but since the soluble dyes do not become agglomerate, the effect of color removal is limited. However, in the present invention, since the soluble dye is converted into the colloidal dye intermediate by hydrolysis in the primary and secondary UASB, chromaticity can be easily removed. In addition, a large amount of organic matter is removed during the aerobic treatment, resulting in a side effect of reducing the amount of chemicals consumed in flocculation. In the present invention, only a small amount of 50 to 60 mg / l of aluminum sulfate (Al ₂ (SO ₄ ) ₃ ), which is a general flocculant, removes about 15% of the chromaticity of the aerobic treated wastewater and at about 45% of CODcr. Remove the degree.

In the case of treating the dyeing wastewater according to the present invention, the total CODcr removal rate of the discharged water after coagulation sedimentation is 90 to 97% and the color removal rate is about 95% based on the dyeing wastewater stock solution. It is a very effective treatment that can replace.

In addition, even if only the UASB, UFPB, aerobic treatment of FIG. 3 and coagulation sedimentation were omitted, the CODcr removal rate was not different, and the chromaticity removal rate was higher than that of the dye wastewater treated through the entire process of FIG. . Therefore, when the user of the present invention selects the process of FIG. 3, the coagulation sedimentation process may be omitted, and only if a very good water quality is desired.

Hereinafter, examples of the present invention will be described. However, the following examples are intended to illustrate the invention and the present invention is not limited to the following examples.

Example 1

In order to determine the capacity of the anaerobic dyeing wastewater treatment prior to the continuous experiment, 300ml of the dyeing wastewater was injected into a 500ml Erlenmeyer flask, and 5ml of the anaerobic digestive supernatant was inoculated and vibrated at 30 ° C to change the color and pH of the wastewater. Analyzed. The results of the analysis are shown in FIG. 4.

In FIG. 4, the color was reduced by about 80%, indicating that the anaerobic treatment method was effective for removing the color of the dyeing wastewater.

Example 2

After confirming the color removal ability of the dyeing wastewater by anaerobic treatment through the batch simple test of Example 1, the laboratory scale of 6L treatment capacity for 2 months / dose for the B dyeing industrial wastewater in Ansan-si and K company dyeing wastewater in Daegu-si (bench scale) ) Continuous experiments were carried out. The average water quality, process composition and experimental method of wastewater are shown in Table 3. The schematic diagram of the process applied to the present Example is as FIG.

Average water quality (mg / l) pH Temp (℃) CODcr BOD SS NH ₃ -N TP 12.5 40 1,850 200 50 8 4 Process composition Inflow-pH adjustment tank-1st UASB-Air contact tank-2nd UASB-Aeration and sedimentation tank-Agglomeration and sedimentation tank-Discharge Experiment method Adjust the pH to 9.5-10 by adding H ₂ SO ₄ in the pH control tank.Put the first and second UASB reaction tanks in a water bath to maintain the temperature at 40 ° C. 10 hours, aerobic reaction tank residence time 12 hours, coagulation tank and settling tank total residence time 3 hours

In order to grasp the color removal effect of each step in the present embodiment, the raw waste water, the primary and the secondary UASB-aeration tank effluent (anaerobic-aerobic treatment), and the final treated water (coagulation sedimentation treatment) in the visible light 400 ~ 700nm range Absorbance was analyzed. The change in absorbance analyzed above is shown in FIG. 6. In Figure 6 it can be seen that through the anaerobic-aerobic treatment, most of the chromaticity is removed and the residual chromaticity is removed through the final drug flocculation settling treatment.

In addition, the CODcr and chromaticity removal rate of the 6-month continuous experiment are shown in Table 4.

division Wastewater Primary UASB Air contact tank 2nd UASB Aeration Coagulation precipitation CODcr (mg / l) 1,850 1,350 - 1,000 200 110 CODcr removal rate By process - 27% - 26% 80% 45% accumulate - 27% - 46% 89% 94% Chromaticity Removal Rate accumulate - 75% - 80% 80% 95% pH 10 7.3 8.5 7.5 8.3 6.1

As can be seen in Table 4, when the dyeing wastewater was treated by the process according to the present invention, CODcr 94% and chromaticity 95% showed very high removal rates.

[Experiment 1]

In order to compare the color removal ability which is the most problematic problem in the dyeing wastewater, the following experiments were performed on the two dyeing wastewater treatment methods proposed in the present invention, and the results of the experiment are shown in Table 5.

Step 1: Treatment Step of FIG.

Step 2: the step of eliminating the coagulation sedimentation at the rear end of the treatment step of FIG.

Experimental Method: The same method as in Example 2 (10 hours residence time of UFPB in Step 2)

Unit: Chromaticity (degrees)

fair enemy Aeration Tank / Sedimentation Tank Runoff Flocculation tank / sedimentation tank effluent Remarks Process 1 800 110 70 Raw water with a chromaticity of 800 is a general dyeing wastewater, and raw water with a chromaticity of 2,839 is a dyeing wastewater containing a large amount of reducing dyes. 2,839 939 493 Process 2 800 60 - 2,839 193 -

As can be seen in Table 5, the color removal ability of the process 2 was found to be superior to that of the process 1, especially in the case of the dye wastewater mixed with a large amount of reducing dye, the process 2 was absolutely excellent. The reason for this is that hydrolyzation of highly reducing reducing dyes proceeded in the activated carbon-filled UFPB applied in Step 2.

Therefore, it is possible to construct an optimal treatment system based on the two processes proposed in the present invention in consideration of the properties and economics of the dyeing wastewater.

As described above, the dyeing wastewater treatment method according to the present invention effectively lowered the chromaticity of the dyeing wastewater, and made it possible to discharge high quality effluent by decomposing the hardly decomposable polymer organic matter present in the dyeing wastewater.

Claims (10)

(a) adjusting the pH of the introduced dye wastewater; (b) hydrolyzing and fermenting the organic acid through the first upflow anaerobic sludge blanket process to adjust the pH adjustment; (c) contacting the dyed wastewater that has passed through the first upflow anaerobic sludge blanket process with air; (d) hydrolyzing and fermenting the organic acid through the second upflow anaerobic sludge blanket process in contact with the air; (e) aerobic treatment of the dyed wastewater that has passed the second upflow anaerobic sludge blanket process; And (f) flocculating the aerobic dyed dye wastewater; Dyeing wastewater treatment method comprising a. (a) adjusting the pH by introducing a dye wastewater containing a large amount of reducing dye; (b) hydrolyzing and fermenting the organic acid through the first upflow anaerobic sludge blanket process to adjust the pH adjustment; (c) hydrolyzing and organic acid fermenting the dyeing wastewater that has passed the first upflow anaerobic sludge blanket process through a second upflow anaerobic sludge blanket process; (d) aerobic treatment of the dyed wastewater having passed through the second upflow anaerobic sludge blanket process; And (e) flocculating the aerobic dyed dye wastewater; Dyeing wastewater treatment method comprising a. (a) introducing a dye wastewater to adjust pH; (b) hydrolyzing and fermenting the organic acid through the first upflow anaerobic sludge blanket process to adjust the pH adjustment; (c) contacting the dyed wastewater that has passed through the first upflow anaerobic sludge blanket process with air; (d) hydrolysis and organic acid fermentation of the dye wastewater contacted with air in an upflow packed bed bioreactor; And (e) aerobic treatment of the dye wastewater that has passed through the upflow packed bed bioreactor; Dyeing wastewater treatment method comprising a. The method of claim 3, further comprising the step of flocculating sedimentation of the dyed wastewater having undergone the aerobic treatment step. The anaerobic hydrolysis of any one of claims 1 to 4, wherein the dyeing wastewater is adjusted to pH 9 to 10 in the step of adjusting the pH of (a), in the first upflow anaerobic sludge blanket process. Dyeing wastewater treatment method characterized in that to proceed in alkaline conditions. The method of any one of claims 1, 3, and 4, wherein the H ₂ S generated in the first upflow anaerobic sludge blanket process is degassed in an air contacting step. The method according to any one of claims 1 to 4, wherein the chemical structure of the dye molecules in the introduced dye wastewater is the first upflow anaerobic anaerobic sludge blanket process, the second upflow anaerobic sludge blanket process or upflow packed phase organisms. Dyeing wastewater treatment method characterized in that it is converted into a colloid or a water-insoluble intermediate in the soluble dye while passing through the reactor to precipitate as a precipitate or removed in the flocculation sedimentation step. The method according to any one of claims 1 to 4, wherein the azo group, which is a color functional group in the introduced dye wastewater, is the first upflow anaerobic sludge blanket process, the second upflow anaerobic sludge blanket process, or the upflow packed bed bioreactor. Dyeing wastewater treatment method characterized in that the reduction is provided by receiving hydrogen provided through anaerobic organic acid fermentation. The method according to any one of claims 1 to 4, wherein the polymer hardly decomposable organic material in the introduced dye wastewater is subjected to the first upflow anaerobic sludge blanket process, the second upflow anaerobic sludge blanket process, or the upflow packed phase organism. Dyeing wastewater treatment method characterized in that the low-molecular-weight organic material is converted in the reaction tank is removed in the aerobic treatment step. The method of claim 3 or 4, wherein the upflow packed bed bioreactor is an upflow packed bed bioreactor filled with activated carbon.